CN103305258A - Method for reducing viscosity of quenching oil of ethylene unit - Google Patents
Method for reducing viscosity of quenching oil of ethylene unit Download PDFInfo
- Publication number
- CN103305258A CN103305258A CN2012100709273A CN201210070927A CN103305258A CN 103305258 A CN103305258 A CN 103305258A CN 2012100709273 A CN2012100709273 A CN 2012100709273A CN 201210070927 A CN201210070927 A CN 201210070927A CN 103305258 A CN103305258 A CN 103305258A
- Authority
- CN
- China
- Prior art keywords
- quenching oil
- oil
- viscosity
- quenching
- ethylene unit
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Abstract
The invention discloses a method for reducing viscosity of quenching oil of an ethylene unit. The method comprises the steps of introducing a stream of quenching oil from the bottom of an oil washing tower, carrying out gas phase counter-current extraction with a solvent in an extraction tower, and separating the product into viscosity reducing quenching oil and a heavier asphalt phase, wherein the viscosity reducing quenching oil returns to the oil washing tower after the temperature is reduced. The method has the beneficial effects that gas phase extraction treatment is carried out on the quenching oil of the ethylene unit with the solvent to remove the asphaltene in the quenching oil to obtain the viscosity reducing quenching oil, and the viscosity reducing quenching oil with low viscosity is returned to the oil washing tower of a quenching system, thus the viscosity of the quenching oil of the ethylene unit can be substantially reduced.
Description
Technical field
The present invention relates to the ethylene production field of petrochemical complex, say further, relate to a kind of method that reduces ethylene unit quenching oil viscosity.
Background technology
At present, mainly adopt in the world the steam heat cracking technology to produce ethene.The raw materials such as lighter hydrocarbons, petroleum naphtha, hydrogenation tail oil and a certain proportion of dilution steam generation are blended in scission reaction occur under the high temperature, go out the industrial chemicals such as ethene, propylene, divinyl through operation final production such as over-quenching, compression, separation.
Quenching system is an important component part of ethylene unit, is comprised of equipment such as quencher, oil scrubber, water wash columns, is bearing the task of separating and cracking gasoline, diesel oil, oil fuel component, also is the key equipment that reclaims heat.As the first operation of cracking of ethylene gas disposal, it usually becomes the bottleneck of restriction ethylene unit output and running steady in a long-term, and its operation quality is to ethylene unit performance important.
The splitting gas that the pyrolyzer outlet comes is sent into the oil scrubber bottom at quencher behind the quenching oil spraying cooling, behind the reflux cooling, the heavy component in the split product is solidifying to be incorporated in the quenching oil at the bottom of tower.Light constituent in the split product enters water wash column and continues to be cooled to about 40 ℃ from the oil scrubber Base top contact, enters follow-up compression separation system.The needed most of dilution steam generation of cracking derives from the UTILIZATION OF VESIDUAL HEAT IN of the inner quenching oil of device, and insufficient section is replenished by pipe network steam.The oil wash column bottom temperature is higher, vapor generation more, and the device by utilizing waste heat utilization is better, and outer benefit steam consumption is fewer.Therefore the height of oil wash column bottom temperature directly determines the size of waste heat recovery amount, also affects the device production cost.Quenching oil constantly circulation between quencher and oil wash tower reactor in the quenching system, its internal circulating load per hour often reaches several kilotons, and the extraction of oil product only has tens tphs, causes quenching oil to be detained for a long time in system.Owing to containing the unsaturated aromatic hydrocarbon components such as vinylbenzene, indenes in the split product quenching oil, polymerization can occur in the circulation under long high temperature of these materials, generates macromolecular substance, causes the increase of quenching oil viscosity, and the quenching oil moving situation is worsened, and affects heat transfer effect.Owing to can't improve by quenching oil viscosity influence oil wash column bottom temperature, cause the quenching oil heat recuperation incomplete, cause dilution steam generation generating capacity wretched insufficiency, therefore need a large amount of steam to fill into system, caused energy dissipation.Because quenching oil viscosity increases, increase the power of systemic circulation pump simultaneously, caused plant energy consumption high.For this reason, each ethene technical patent merchant has taked various viscosity reducing technologies to process.
Traditional process for reducing viscosity is to add modified thinning oil to reduce viscosity.The Pyrolysis gas oil PGO blending is to quenching oil, though can play the effect that reduces the quenching oil viscosity, also Shortcomings part.At first, can increase the internal circulating load of Pyrolysis gas oil PGO in gasoline splitter, strengthen the gasoline splitter tower reactor to the gas phase load at tower middle part, correspondingly reduce the processing power of gasoline splitter; Secondly, contain the components such as a large amount of vinylbenzene, naphthalene, indenes in the Pyrolysis gas oil PGO, when they along with the quenching oil circulation time, can produce polymkeric substance by polymerization reaction take place, and accumulate on the column plate or filler of gasoline splitter, affect heat transfer and the mass transfer effect of column plate and filler, tower pressure reduction is risen, the processing power of tower descends; Again, owing to the increase of Pyrolysis gas oil PGO internal circulating load, can contain the component of part diesel oil in the Pyrolysis fuel oil PFO of the pyrolysis gasoline of cat head and tower reactor extraction, have influence on the quality of pyrolysis gasoline and oil fuel, meeting when serious is so that the operation deterioration of follow-up quenching water column; At last, because the amount of quenching oil is very large, thus in order to reduce the chilling oil viscosity, usually need to mix a large amount of Pyrolysis gas oil PGOs, and the time of injecting is longer, otherwise the visbreaking effect is relatively poor.
Viscosity depressant be in recent years both at home and abroad research department and ethene patent merchant work out the chemical agent of various suitable reduction quenching oil viscosity, the activity that suppresses the polyreaction free radical by adding chemical assistant realizes the visbreaking target.CN 101062880A proposes a kind of quench oil viscosity reductant that is comprised of stopper, dispersion agent and metal passivator, have and suppress polymerization, prevent from assembling and the effect of passivating metallic surfaces, reduce corrosion and the fouling of quenching system equipment, add-on is few, and have satisfactory stability, can not produce the side effect of oil-water emulsion.
Visbreaking tower visbreaking principle is, from the quenching oil of quenching oil circulation pump outlet, under the control of temperature control valve (TCV), the ethane cracking gas that comes with Control for Pyrolysis Furnace Area contacts in nozzle mixer, and the light constituent in the quenching oil is vaporized, and enters the visbreaking tower with splitting gas.The visbreaking tower is made of two sections, and epimere is a cyclonic separator, and hypomere is a free-falling district.After mixture enters the visbreaking tower, at first in cyclonic separator, carry out the separation of liquid phase, the light constituent of vaporizing in ethane cracking gas and the quenching oil enters the oil scrubber tower reactor from the visbreaking column overhead, the heavy liquid phase component of vaporization is not passed through hypomere, enter visbreaking tower tower reactor, output to the tank field as byproduct (Pyrolysis fuel oil PFO).Like this, from quenching oil, fractionate out the heavier feeds that contains a large amount of resin and asphalts selectively and light material is stayed in the system, the light component concentration in the quench oil circulated is increased, thereby reduce the quenching oil viscosity.Utilize ethane outlet of still splitting gas or directly use the steam stripped mode of steam heat, by the light constituent stripping in the quenching oil is turned back in the recycle system, the high oil of lightweight oil dilution proportion viscosity realizes visbreaking in the utilization increase quenching oil recycle system, to guarantee system stable operation.The control method of quench oil circulated viscosity is in the cracking fractionation plant that CN1220987 proposes, the pyrolyzer effluent is contacted with the quenching oil slip-stream of 0.1-0.5kg/kg, the vapour-liquid mixture that separate to obtain to be removing tarry liquid, and the steam that stays is given to oil scrubber.Remove tarry liquid from the oil scrubber feed by this way, so that oil scrubber operation backflow is less, bottom temp is higher, and reclaims more heat under comparatively high temps.The weak point of the method is: the one, and when burning, the ethane stove must use the high compressed steam air lift, and gas phase is directly returned quenching oil column, and the quenching oil column load is high; The 2nd, send in the heavy fuel oil light constituent content behind the stripping outside less, send pipeline outside and easily stop up.From the condition of production of each cover ethylene unit, only have minority ethylene unit Reduce viscosity tower normal operation and reach certain visbreaking effect.Because the operation of visbreaking system is undesired, there are larger gap in the actual motion index of most of device quench oil system and original design value, become the bottleneck of limit production ability.Adopt the steam stripped process for reducing viscosity of water vapor in actually operating, in fact all can not normally move owing to heavy fuel oil stops up in the visbreaking tower reactor.
The splitting gas that CN101074184 proposes the pyrolyzer outlet is come is sent into the oil scrubber bottom after cooling, carry out separating substances, forms three bursts of backflows; Quenching oil is after cooling at the bottom of the tower, and part is returned oil scrubber, and part is sent outside; Oil is coiled after cooling in the stage casing, and part is returned oil scrubber, and part is used as adjusting viscosity at the bottom of being blended into tower, and part is sent outside; Trim the top of column gasoline enters through pipeline, and pyrolyzer sends into rear system after the logistics cooling the most at last.This method has only been optimized the oil scrubber temperature distribution, does not change quenching oil and forms, and is little to reducing the viscosity effect, and increased oil scrubber stage casing load, affects throughput.
Though aforesaid method can play the effect that reduces the quenching oil viscosity, can't fundamentally solve the high problem of quenching oil viscosity.Quenching oil is as the important heat-transfer medium of ethylene unit, and the rising of its viscosity can directly have influence on the normal running of pyrolyzer, gasoline splitter and dilution steam generation generation systems, even quenching oil recycle system pipeline and equipment obstruction accident occur.Quench oil system the steady running of ethylene unit long period high loading and energy-saving and cost-reducing play a part very important.Domestic a lot of ethylene units all exist the Reduce viscosity system design reasonable not at present, the quenching oil viscosity is high, and the quenching oil column tower top temperature is higher, the tower reactor temperature is on the low side, Reduce viscosity system fluctuation of service, heat recovery efficiency is low, the problems such as often emulsification of quenched water.Guaranteeing that from technological design quench oil system is comprised of and operational condition suitable material, will take innovative approach to irrational visbreaking technique, is the key point of assurance system continuous and steady operation.
Summary of the invention
For solving problems of the prior art, the invention provides a kind of method that reduces ethylene unit quenching oil viscosity, quenching oil removes wherein bituminous matter by the extracting of solvent gas phase, thereby reduces viscosity.
The purpose of this invention is to provide a kind of method that reduces ethylene unit quenching oil viscosity.
Comprise:
Quenching oil from the oil scrubber bottom obtains the visbreaking quenching oil behind the gas phase countercurrent extraction.
Particularly,
Draw one quenching oil at the bottom of the oil scrubber tower, with solvent gas phase countercurrent extraction in extraction tower, be separated into visbreaking quenching oil and heavier pitch mutually, the visbreaking quenching oil returns oil scrubber after reducing temperature.
Described solvent is to be selected from C
2-C
4A kind of or its mixture of alkane or alkene; Be preferably a kind of or its mixture in C3-C4 alkane or the alkene;
The quenching oil feeding temperature is 150-230 ℃, and the solvent feed temperature is 90-250 ℃, and the weight ratio of solvent and quenching oil is 0.1-5, is preferably 0.5-2;
The pressure of described extraction tower is 0.1MPa-1MPa, and temperature is 90 ℃-250 ℃;
Described visbreaking quenching oil reduces the temperature to 110-140 ℃, reduces pressure extremely than returning the quenching oil column middle part behind the large 0-0.1Mpa of oil scrubber pressure.
Specifically can be by the following technical solutions:
Draw one quenching oil at the bottom of the oil scrubber tower, with solvent gas phase countercurrent extraction, cat head is isolated lighter oil phase in the gas phase extraction tower, and tower reactor is isolated heavier pitch phase.Behind the pitch phase desolvation as oil fuel or asphaltic products. extraction.The visbreaking quenching oil returns oil scrubber after reducing temperature and pressure.
Described quenching oil is the oil distillate of oil scrubber tower reactor in the ethylene unit quenching system, its typical composition is polycyclic aromatic hydrocarbons, colloid, bituminous matter, described ethylene unit mainly by industrial pyrolysis furnace and chilling, compression, the system such as separate and consist of, quenching system mainly comprises quencher, oil scrubber, water wash column.
The gas extraction tower mainly comprises rotating disc contactor or sieve-tray tower or packing tower.
The present invention is a kind of gas method for extracting that reduces ethylene unit quenching oil viscosity, process by the ethylene unit quenching oil being carried out the extracting of solvent gas phase, remove bituminous matter wherein, obtain the visbreaking quenching oil, the visbreaking quenching oil of this low-viscosity is returned the quenching system oil scrubber, but decrease ethylene unit chilling oil viscosity thus.
Description of drawings
Fig. 1 method schematic diagram of the present invention
Description of reference numerals:
101 extraction towers; 12 quenching oils; 13 solvents; 21 visbreaking quenching oils; 22-pitch phase
Embodiment
Below in conjunction with embodiment, further specify the present invention.
As shown in Figure 1, draw one quenching oil 12 at the bottom of quenching oil column, quenching oil 12 enters extraction tower 101, and gas-solvent 13 enters from extraction tower 101 bottoms, and quenching oil is carried out the extracting of adverse current gas phase.Charging is separated into visbreaking quenching oil 21 and heavier pitch mutually 22, and visbreaking quenching oil 21 is discharged by extraction tower 101 cats head, and pitch is mutually 22 by discharging at the bottom of extraction tower 101 towers.As oil fuel or asphaltic products. extraction, after reducing temperature, visbreaking quenching oil 21 returns oil scrubber behind pitch phase 22 desolvations.
Embodiment:
Draw one quenching oil from the ethylene unit quenching oil recycle system, its temperature is 170 ℃, and pressure is 0.16MPa, and its viscosity is 1500mm
2/ s.
The propane solvent temperature is 250 ℃, and pressure is 0.16MPa.The propane critical temperature is 96.7 ℃, and emergent pressure is 4.25MPa.
Extraction tower is sieve-tray tower, the pressure 0.16MPa of extraction tower, and quenching oil enters extraction tower top, and the propane solvent that quenching oil weight is 0.2 times enters the extraction tower bottom, 250 ℃ of tower top temperatures, 250 ℃ of tower reactor temperature.Cat head is isolated the visbreaking quenching oil, isolates heavier pitch phase at the bottom of the tower.After pitch was depressurized to the normal pressure desolvation mutually, oily extraction acted as a fuel.
Obtaining visbreaking quenching oil viscosity from the separation of gas extracting cat head is 15mm
2/ s, visbreaking quenching oil cool to 120 ℃ and return ethylene unit quenching system oil scrubber middle part.
Comparative Examples:
Existing visbreaking tower process is for to draw one quenching oil from the ethylene unit quenching oil recycle system, and its temperature is 195 ℃, and pressure is 0.16MPa, and its viscosity is 1500mm
2/ s.Ethane stove splitting gas temperature is 500 ℃, and pressure is 0.16MPa.This quenching oil and ethane stove splitting gas are mixed into the visbreaking tower, and the visbreaking pressure tower is 0.16MPa, and temperature is 272 ℃, and the cat head separation obtains the visbreaking quenching oil, isolates heavy fuel oil at the bottom of the tower.(viscosity is 65mm to 272 ℃ visbreaking quenching oil
2/ s) enter the oil scrubber bottom.Existing method has been lost the higher-grade heat energy of ethane stove splitting gas, also is taken in the quenching system, has increased energy consumption.
Data by embodiment and Comparative Examples can find out, the visbreaking chilling oil viscosity that embodiment obtains is starkly lower than Comparative Examples, and visbreaking effect of the present invention is excellent.
Claims (9)
1. method that reduces ethylene unit quenching oil viscosity is characterized in that described method comprises:
Quenching oil from the oil scrubber bottom obtains the visbreaking quenching oil behind the gas phase countercurrent extraction.
2. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 1 is characterized in that described method comprises:
Draw one quenching oil at the bottom of the oil scrubber tower, with solvent gas phase countercurrent extraction in extraction tower, be separated into visbreaking quenching oil and heavier pitch mutually, the visbreaking quenching oil returns oil scrubber after reducing temperature.
3. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 2 is characterized in that:
Described solvent is to be selected from C
2-C
4A kind of or its mixture of alkane or alkene.
4. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 3 is characterized in that:
Described solvent is a kind of or its mixture in C3-C4 alkane or the alkene.
5. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 2 is characterized in that:
The quenching oil feeding temperature is 150-230 ℃, and the solvent feed temperature is 90-250 ℃, and the weight ratio of solvent and quenching oil is 0.1-5.
6. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 5 is characterized in that:
The weight ratio of described solvent and quenching oil is 0.5-2.
7. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 2 is characterized in that:
The pressure of described extraction tower is 0.1MPa-1MPa, and temperature is 90 ℃-250 ℃.
8. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 4 is characterized in that:
The quenching oil feeding temperature is 150-230 ℃, and the solvent feed temperature is 90-250 ℃, and the weight ratio of solvent and quenching oil is 0.5-2; The pressure of described extraction tower is 0.1MPa-1MPa, and temperature is 90 ℃-250 ℃.
9. the method for reduction ethylene unit quenching oil viscosity as claimed in claim 2 is characterized in that:
Described visbreaking quenching oil reduces the temperature to 110-140 ℃, reduces pressure extremely than returning the quenching oil column middle part behind the large 0-0.1Mpa of oil scrubber pressure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210070927.3A CN103305258B (en) | 2012-03-16 | 2012-03-16 | Method for reducing viscosity of quenching oil of ethylene unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210070927.3A CN103305258B (en) | 2012-03-16 | 2012-03-16 | Method for reducing viscosity of quenching oil of ethylene unit |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103305258A true CN103305258A (en) | 2013-09-18 |
| CN103305258B CN103305258B (en) | 2015-06-17 |
Family
ID=49130984
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210070927.3A Active CN103305258B (en) | 2012-03-16 | 2012-03-16 | Method for reducing viscosity of quenching oil of ethylene unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103305258B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105567290A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105567291A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105567295A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing energy consumption of ethylene device |
| CN105567293A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105566029A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101323553A (en) * | 2007-06-13 | 2008-12-17 | 中国石油天然气股份有限公司 | Method for improving ethylene apparatus quench oil tower bottom temperature |
| CN101962565A (en) * | 2010-10-19 | 2011-02-02 | 惠生工程（中国）有限公司 | Quench oil viscosity reducing process for two quench oil systems |
| WO2011081601A1 (en) * | 2009-12-30 | 2011-07-07 | Irpc Public Company Limited | Methods and processes for producing process oils with a low polyaromatic hydrocarbon content |
-
2012
- 2012-03-16 CN CN201210070927.3A patent/CN103305258B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101323553A (en) * | 2007-06-13 | 2008-12-17 | 中国石油天然气股份有限公司 | Method for improving ethylene apparatus quench oil tower bottom temperature |
| WO2011081601A1 (en) * | 2009-12-30 | 2011-07-07 | Irpc Public Company Limited | Methods and processes for producing process oils with a low polyaromatic hydrocarbon content |
| CN101962565A (en) * | 2010-10-19 | 2011-02-02 | 惠生工程（中国）有限公司 | Quench oil viscosity reducing process for two quench oil systems |
Non-Patent Citations (1)
| Title |
|---|
| 许斌: "乙烯装置急冷系统工艺模拟与研究", 《天津大学硕士学位论文》, 30 June 2006 (2006-06-30), pages 60 - 72 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105567290A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105567291A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105567295A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing energy consumption of ethylene device |
| CN105567293A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105566029A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | Method for reducing ethene device energy consumption |
| CN105567290B (en) * | 2014-10-14 | 2017-06-30 | 中国石油化工股份有限公司 | A kind of method for reducing ethylene unit energy consumption |
| CN105567291B (en) * | 2014-10-14 | 2017-09-29 | 中国石油化工股份有限公司 | A kind of method for reducing ethylene unit energy consumption |
| CN105566029B (en) * | 2014-10-14 | 2017-09-29 | 中国石油化工股份有限公司 | A kind of method for reducing ethylene unit energy consumption |
| CN105567295B (en) * | 2014-10-14 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of method for reducing ethylene unit energy consumption |
| CN105567293B (en) * | 2014-10-14 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of method for reducing ethylene unit energy consumption |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103305258B (en) | 2015-06-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103305257B (en) | Method for reducing viscosity of quenching oil of ethylene unit | |
| CN103305259B (en) | A kind of method reducing ethylene unit quenching oil viscosity | |
| CN103305260B (en) | A kind of system and method reducing ethylene unit quenching oil viscosity | |
| CN103305258B (en) | Method for reducing viscosity of quenching oil of ethylene unit | |
| CN102533322B (en) | Method for producing propylene by using Fischer Tropsch synthetic oil in catalytic cracking mode | |
| Wu | Acidic and basic catalytic cracking technologies and its development prospects for crude oil to chemicals | |
| JP2022523128A (en) | Hydrocarbon-catalyzed conversion method of downflow reactor and its equipment | |
| CN1119389C (en) | Coking delay process for lowering foam layer in coke tower | |
| CN105566029B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN104449807B (en) | A kind of quenching oil extracting visbreaking system | |
| CN105567292B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN102796556B (en) | A kind of catalysis conversion method of petroleum hydrocarbon | |
| CN105567290B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN104449820A (en) | System for reducing ethylene unit quenching oil viscosity and method for improving solvent recovery rate | |
| CN104449808A (en) | System and method for reducing ethylene unit quenching oil viscosity | |
| CN1141361C (en) | Catalytic cracking process for reducing content of olefin in gasoline | |
| CN104449827A (en) | System and method for reducing ethylene unit quenching oil viscosity | |
| CN105567294B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN104449826A (en) | Method for reducing ethylene unit quenching oil viscosity | |
| CN104449825B (en) | A kind of method reducing ethylene unit quenching oil viscosity and improve solvent recovering rate | |
| CN105567291B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN105567295B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN105567296B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN105505436B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN105567293B (en) | A kind of method for reducing ethylene unit energy consumption |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |